Method and apparatus for super critical treatment of liquids

ABSTRACT

A process for sterilization of a liquid in a continuous system including a series of steps. First the liquid is continuously pumped into a pressurized system. Second, the pressure on the liquid is increased in a first pressurization stage. Next, the liquid is increased in pressure in a second pressurization stage. Fourth, the liquid is held at an elevated pressure for a predetermined period of time to kill off microorganisms within the liquid. The liquid is then rapidly depressurized to fracture microorganisms within the liquid. The apparatus for producing this process includes a continuous liquid treatment system with a pump, a first stage intensifier, a surge drum, a second stage intensifier, a pressure receiver and a pressure reducer. A particulate treatment system may also be included which includes a pressure receiver, an intensifier, and a recoverer for blending a particulate component with the liquid component.

FIELD OF THE INVENTION

The present invention relates to a super critical treatment process forthe sterilization or deactivation of microorganisms in liquids, such asliquid foods and beverages.

BACKGROUND OF THE INVENTION

Many liquids, such as commercial processed foods, including, but notlimited to, juices, beverages, soups and stews, contain microorganismsthat continue to multiply after processing, thereby reducing the safeshelf life of the foods. It is has been known that exposure ofmicroorganisms to very high pressures (e.g. up to 100 kpsi) will reducethe population of various species of microorganisms during batchprocessing. Furthermore, the high pressure treatment of liquid foods,while deactivating microorganisms, has essentially no negative effect onthe taste and appearance of the liquid.

The prior art generally discloses complicated batch processes andapparatus for the deactivation of microorganisms in a liquid.Unfortunately, batch processes can be expensive and inefficient.

SUMMARY OF THE INVENTION

In accordance with the teachings of the present invention, a process andan apparatus for the sterilization of a liquid are provided whichsubstantially eliminate or reduce disadvantages and problems associatedwith prior art devices and techniques. In particular, the process forsterilizing a liquid (which may be a liquid component alone or a liquidcomponent and a particulate component) includes increasing the pressureon the liquid, and rapidly reducing the pressure on the liquid componentwhile maintaining the liquid within an acceptable temperature range.

To produce this process, there is provided an apparatus that includes apump for introducing a liquid into a pressurized system. The pump iscoupled with a first stage intensifier for increasing the pressure ofthe liquid. A second stage intensifier is coupled to the first stageintensifier to further increase the pressure on the liquid. Although thetwo-stage increase is preferred, a single stage could also be used. Apressure receiver is connected to the second stage intensifier, thepressure receiver for maintaining the pressure on the liquid for apredetermined period of time. Finally, a pressure reducer is attached tothe pressure receiver wherein the pressure reducer receives the liquidand reduces the pressure on the liquid to atmospheric pressure. Inaddition, a particulate component treatment apparatus can be provided,which includes a receiver, an intensifier, and a mixer, for mixing theparticulate component with the liquid component, if particulatecomponents are provided. The particulate component treatment apparatuscan also be used on the liquid components, and thus a mixer may not beneeded in such cases.

One important technical advantage of the present invention is the factthat it provides a continuous system for sterilizing a liquid, therebyreducing the strain on the apparatus from the repeated cycling ofpressurization in the system, and increasing system efficiency. Anotherimportant technical advantage of the present invention is that it can berepaired without interrupting the continuous process for sterilizationof liquid within the system.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a block flow diagram of the total deactivation process.

FIG. 2 is a block flow diagram of the supercritical pressure liquidtreatment process.

FIG. 3 is a schematic diagram of the liquid supercritical pressuretreatment apparatus.

FIG. 4 is a schematic diagram of the supplemental maintenance controlsystem.

FIG. 5 is a schematic cross sectional view of stainless steel lined highpressure tubing.

FIG. 6 illustrates the intensifier system pressure relief system.

FIG. 7 is a schematic view of the pressure let down station.

FIG. 8 is a is a cross sectional drawing of the design for acontrollable high pressure high velocity pressure/flow control valve.

FIG. 9 is a cross-sectional view of orifice pressure/flow controlsystem.

FIG. 10 illustrates the thermodynamics of the pressure let down station.

FIG. 11 is a block flow diagram showing the particulate treatmentprocess.

FIG. 12 is a schematic diagram of the single receiver configuration ofthe particulate treatment apparatus.

FIG. 13 is a schematic diagram of the multiple receiver configuration ofthe particulate supercritical pressure treatment apparatus.

FIG. 14 is a cross sectional diagram illustrating the pulp treatmentbatch receiver.

FIG. 15 is a cross sectional drawing of a Graylock coupling used toconnect the lined high pressure process tubing.

FIG. 16 is a cross sectional drawing of a first pressurization end plugfor the treatment apparatus.

FIG. 17 is a cross sectional drawing of a second pressurization end plugfor the treatment apparatus.

DETAILED DESCRIPTION OF THE INVENTION

Throughout the following discussion, specific pressures, temperatures,times, and other parameters, and specific ranges for such parameters,are provided. It should be understood that these are exemplary only, andthat others can be used without departing from the intended scopeherein.

The present invention relates to a process and an apparatus for theprocess of treating liquid foods and beverages, including, but notlimited to, juices, fruit juices, orange juice, grapefruit juice,tangerine juice, apple juice, stews, and beef stew. The liquid, and, ifany, particulate components, in this system is pressurized anddepressurized to increase the shelf life of the liquid once packaged. Inthe preferred embodiment, the pressure on the liquid (and particulatecomponents, if any) in the system is increased to about 60,000 psig andheld for a sufficient period of time (e.g., about 100 to about 500seconds) to effect the desired kill level of microbial population withinthe liquid. After the liquid food has been pressurized, it is rapidlydepressurized to cause the remaining microbes within the liquid food tofracture. To maintain the integrity and taste of the liquid, thetemperature for the liquid food in the process and the apparatus ismaintained within a desired temperature range, preferably between about35 degrees Fahrenheit and about 85 degrees Fahrenheit.

Turning now to FIG. 1, a flow chart is provided to illustrate a processaccording to the present invention. The illustrated process involves aliquid and a particulate component, it being understood that the presentinvention also applies in cases where there is only a liquid component.

As illustrated in FIG. 1, the process begins with step A whereinuntreated liquid food of approximately 10% particulate component isintroduced into the pressurized system. The liquid food is thenseparated into a liquid component and a particulate component in step Bvia a separator. The liquid and particulate components are each sent forseparate pressure treatments in steps C and D respectively. Once theliquid and particulate matter have been pressure treated, the twocomponents are blended in step E. Finally, this bulk product is packagedfor storing in step F.

FIG. 2 illustrates step C of FIG. 1, in which the liquid is treated in acontinuous (as opposed to batch) process. Step C1 in this processinvolves introducing the liquid component into a continuous system forthe pressurization and depressurization of the liquid component. Next,in step C2, the liquid reaches a first stage in the system whereby thepressure on the liquid increases to a first pressure, which may be about30,000 psig, as the liquid flows through the system. In step C3, theliquid reaches a second stage in the system whereby the pressure on theliquid increases to a second pressure, which may be about 60,000 psig,as the liquid flows through the system. Pressurizing the liquidcomponent in two stages facilitates continuous treatment. However, itshould be understood that pressure could be increased at a single stagewithout departing from the intended scope herein. In step C4, the liquidcomponent is processed at the second pressure for a time sufficient toaffect a desired microbial kill level (for example, between about 100and 300 seconds). At this pressure, the original volume of liquidcomponent is reduced.

In steps C5-C12 the liquid is introduced into a third stage in thesystem whereby volume of the liquid is increased while the pressure onthe liquid is reduced to a third pressure, such as atmospheric pressure.In a particular embodiment, the pressure reduction occurs through aseries of steps to keep the liquid within a desired temperature range,so as to minimize temperature-induced off-tastes. Exemplary steps areillustrated in C5-C12. It should be understood, however, that more orless (including only one) of these steps may be used without departingfrom the intended scope herein.

In step C5 the pressurized liquid in the system is cooled to about 35degrees Fahrenheit. Step C6 involves reducing pressure on the liquid toabout 41,000 psig, for example, by a reverse Joule-Thompson effect,whereby as the pressure in the system reduces and the liquid expands,the temperature in the liquid increases. Therefore, as the pressure onthe liquid is reduced, the temperature of the liquid in the systemincreases, for example, to about 85 degrees Fahrenheit for a change fromabout 60,000 to about 41,000 psig. Step C7 involves cooling the liquidagain back to 35 degrees Fahrenheit. In step C8, the pressure of theliquid is again reduced, for example, to about 21,000 psig. Again, thiscauses the temperature of the liquid to increase. Step C9 involvescooling the liquid back to 35 degrees Fahrenheit. In step C10, thepressure of the liquid is again reduced to about 1,500 psig. Step C11involves again cooling the liquid, for example, to 35 degreesFahrenheit. Finally, in step C12, the pressure of the liquid is againreduced, this time to atmospheric pressure. In step C12 the liquidcomponent is then sent to a liquid component and particulate componentmixer, if a particulate component is provided.

The temperatures, pressures, and times illustrated in the above example,and below, may be changed, depending on the desired costs, temperaturesensitivity of the liquid, and other considerations.

To fully treat the liquid component material in the process describedabove, there is provided in FIG. 3 a supercritical liquid treatmentapparatus 1. More particularly, FIG. 3 shows a liquid component feedline 10 having a block valve 10a. Liquid component feed line 10 connectsto a liquid feed pump 12 whereby the liquid component feeds into liquidfeed pump 12 at a temperature of 35 degrees Fahrenheit and a pressure of20 psig. In addition, connected to line 10 is hot water line 14containing valve 14a located between line 10 and hot water tank 16.During the treatment of the liquid component, valve 14a on hot waterline 14 is closed. Liquid feed pump 12 increases the pressure of theliquid component to 500 psig and temperature to 37 degrees Fahrenheitand pumps the liquid component into line 20. Line 20 splits into threeseparate lines 22, 24 and 26 wherein lines 22 and 24 feed intointensifier 30 while line 26 is a release (or surge) line.

The first intensifier comprises a first cylinder 34a and a secondcylinder 34b connected to hydraulic power chambers 36a and 36brespectively. Plungers 38a and 38b are disposed within cylinders 34a and34b respectively. Hydraulic power package 50 is connected to cylinders34a and 34b via lines 52 and 54 respectively. Lines 52 and 54 allowhydraulic fluid to flow from power chambers 36a and 36b to hydraulicpower package 50 and then back again. Power package 50 controls themovement of plungers 38a and 38b within cylinders 34a and 34b by theflow of hydraulic fluid through valves 56 and 58 located within powerpack 50. The pressure of the hydraulic fluid in lines 52 and 54 isbetween about 1,800 psig and about 3,000 psig.

For example, pack 50 drives plungers 38a and 38b from point B to point Aby simultaneously drawing hydraulic fluid from power chamber 36b anddriving hydraulic fluid into power chamber 36a. As hydraulic fluidenters power chamber 36a, it drives plunger 38a through its compressionstroke from point B to point A. Accordingly, as hydraulic fluid leavespower chamber 36b, plunger 38b is drawn from point B to point A and isin its suction stroke. When plungers 38a and 38b reach point A, valves56 and 58 in power package 50 reverse themselves causing plungers 38aand 38b to reverse direction and move towards position B whereby plunger38a is now in a suction stroke and plunger 38b is in a compressionstroke.

To fill the cylinders of intensifier 30 the liquid component ispressurized at 500 psig so it can serve as a positive feed into thecylinders of the intensifier 30 when the plungers in their cylinder arein their suction stroke. For example, the pressurized liquid in processline 22 feeds into first cylinder 34a when plunger 38a is in a suctionstroke. In addition, pressurized liquid in process line 24 feeds intocylinder 34b when plunger 38b is in a suction stroke.

To maintain a constant pressure in first intensifier 30, there isprovided a release line 26 connected to process line 20 beforeintensifier 30. Along release line 26 is pressure control valve 26a.Pressure control valve 26a is designed so that when pressure insideintensifier 30 exceeds certain pressure, such as about 30,000 psig,pressure control valve 26a will open, allowing additional liquid to flowdown release line 26 and eventually into surge tank 40. The level of theliquid in surge tank 40 will vary, and an inert ballast gas (e.g.,nitrogen) is provided in tank 40 via gas tank 42 which is connected tosurge tank 40 through line 44. The liquid inside surge tank 40 may berecycled through the system and back into pump 10 through recycling line46.

The movement of these plungers in the cylinder through their compressionstroke increase the pressure of the liquid in the system to about 30,000psig. Plungers 38a and 38b, upon movement through the compressionstroke, force the pressurized liquid, in cylinders 34a and 34b throughlines 70 and 72 respectively, and into surge drum 76. The pressure onthe liquid when it enters surge drum 76 is about 30,000 psig, and theincrease in pressure on this liquid is also accompanied by an increasein temperature, to about 57 degrees Fahrenheit at about 30,000 psig.

The liquid in surge drum 76 serves as a pressurized feed into flow line80. Flow line 80 then splits into lines 84 and 88. Both lines 84 and 88split such that line 84 now continues parallel to line 94, and line 88continues parallel to line 98. All four lines feed into a second stageintensifier unit comprising a first intensifier 110 and a secondintensifier 120 connected in parallel with each other. For example,lines 94 and 98 connect to intensifier 110 and lines 84 and 88, runningparallel to lines 94 and 98 respectively, connect to intensifier 120.

While the present embodiment of the invention discloses a second stageintensifier unit that comprises two intensifiers 110 and 120 connectedin parallel with each, other embodiments, for example a singleintensifier, may be used without departing from the intended scopeherein. This parallel design is created to more efficiently handlecapacities greater than 50 gpm and pressures greater than 2750 bar.Furthermore, although the preferred embodiment discussed herein includestwo intensifier stages (intensifier, 30 and second stage intensifierunit (110 and 120)), one pressure increase stage may also be used, forexample with a single intensifier or single intensifier unit of parallelintensifiers.

Intensifier 110 comprises cylinders 114a and 114b for housing plungers118a and 118b while intensifier 120 comprises cylinders 124a and 124bfor housing plungers 128a and 128b. Similar to first stage intensifier30, the plungers in second stage intensifiers 110 and 120 movereciprocal to each other within their respective cylinders. In addition,plunger movement in intensifiers 110 and 120 are controlled by hydraulicpower pack 130.

For example, the liquid that flows into second stage intensifier 110leaves surge drum 76, flows through lines 80, then through lines 84 and88 until lines 84 and 88 join lines 94 and 98. The fluid flows intolines 94 and 98 and alternately enters cylinders 114a, and 114b, whenplungers 118a and 118b are in their suction stroke. Plunger 118a is inits suction stroke when plungers 118a and 118b move from position A toposition B within cylinders 114a and 114b. Accordingly, plunger 118b isin its compression stroke. When plungers 118a and 118b move back fromposition B to position A plunger 114b is now in its suction stroke whileplunger 114a is in its compression stroke.

For the liquid that flows into second stage intensifier 120, thepressurized liquid leaves surge drum 76, through line 80, next flowsinto lines 84 and 88, and enters cylinders 124a, and 124b when plungers128a and 128b are in their suction stroke. Plunger 128a is in itssuction stroke when plungers 128a and 128b move from position A toposition B within cylinders 124a and 124b. Accordingly, plunger 128b isin its compression stroke. When plungers 128a and 128b move back fromposition B to position A, plunger 128b is now in its suction strokewhile plunger 128a is in its compression stroke.

Hydraulic power pack 130 controls the flow of the plungers inside secondstage intensifiers 110 and 120. Lines 142 and 144 connect hydraulicpower pack 130 to power chambers 116a and 116b, while lines 146 and 148connect hydraulic power pack 130 to power chambers 126a and 126b. Thepressure of the hydraulic fluid in lines 142, 144, 146 and 148 isbetween about 1,800 psig and about 3,000 psig. As disclosed above,hydraulic power pack 130 controls the movement of the plungers in thecylinders such that when a compression stroke is completed, valves 132and 134 in hydraulic power pack 130, are reversed causing theintensifier plungers to move in the opposite direction.

Second stage intensifiers 110 and 120 increase the pressure of theliquid to about 60,000 psig. This increase in pressure will also resultin the liquid increasing in temperature to approximately 83 degreesFahrenheit.

Plungers 118a and 118b alternately force the discharge of the compressedliquid through lines 160 and 162 during their compression stroke.Similarly, plungers 128a and 128b alternately force the compressedliquid through lines 170 and 172 during the compression stroke ofplungers 128a and 128b. Lines 160 and 162 then meet and form line 166while lines 170 and 172 meet and form line 176. Lines 166 and 176 thenjoin line 180.

The system may require periodic maintenance, therefore, an additionalembodiment of the invention is shown in FIG. 4 whereby the liquidcomponent treatment system is provided with a supplemental maintenancecontrol system. This system is similar to the system described in FIG. 3however, this system contains an additional series of lines and blockvalves. For example, the system contains an additional line 200 whichconnects to line 20 before valve 20a on line 20. Line 200 extends fromline 20 and connects to lines 94 and 98. Line 200 contains valves 200aand 200b with valve 200a located between line 20 and line 94 and valve200b located between line 94 and line 98. In addition the system isprovided with a Line 210 which connects to surge drum 76 and extends toline 166. Line 210 contains valves 210a and 210b.

This system also contains an additional series of block valves. Forexample, lines 70 and 72 contain valves 70a and 72a respectively. Lines84 and 94 contain valves 84a and 94a located on their respective linesafter line 94 separates from line 84. Similarly, lines 88 and 98 containvalves 88a and 98a located on their respective lines after line 98separates from line 88. Lines 142, 144, 146 and 148 contain valves 142a,144a, 146a, and 148a respectively. Line 166 contains valve 166a betweenline 210 and line 180. Line 180 contains valve 180a between line 176 andline 166.

These additional lines and valves can be opened or closed to allow aseries of repairs to intensifiers 30, 110 and 120. During normaloperating conditions, valves 200a, 200b on line 200, and 210a and 210bon line 210 are closed while all other valves are open. However, when itis necessary to repair intensifier 110, valves 94a and 98a are closedpreventing the liquid component from flowing through lines 94 and 98 andinto intensifier 110. In addition, valves 142a and 144a on lines 142 and144 are closed preventing hydraulic fluid from flowing from intensifier130 into hydraulic chambers 116a and 116b. The closure of these valvesthen frees intensifier 110 to be repaired while the system is stillrunning.

When repairs to intensifier 120 are necessary, valves 84a and 88a areclosed, preventing the liquid component from flowing through lines 84and 88 and into intensifier 120. In addition, valves 146a and 148a areclosed on lines 146 and 148 preventing hydraulic fluid from flowing fromintensifier 130 into hydraulic chambers 126a and 126b. The closure ofthese valves then leaves intensifier 120 free to be repaired while thesystem is still running.

When it is necessary to repair intensifier 30, valve 20a is closed andvalves 200a and 200b are opened to allow fluid into line 200 of thesystem. The fluid then feeds alternatively into lines 94 and 98 and theninto cylinders 114a and 114b of intensifier 110 during their suctionstroke. The pressurized liquid flows into lines 160 and 162 and thenflows into line 166. Line 166 joins line 210 whereby when valves 210aand 210b on line 210 are open and valve 166a on line 166 is closed, thefluid flows into surge drum 76. Valves 70a and 72a are closed to preventflow of the liquid component from surge drum 76 into lines 70 and 72.The fluid in surge drum 76 then serves as a pressurized feed intointensifier 120. This is because valves 94a and 98a on lines 94 and 98are closed preventing the fluid from flowing into intensifier 110. Thissituation then leaves intensifier 30 free to be repaired while thesystem is still running.

Once the liquid component is pressurized, for example to about 60,000psig by intensifiers 110 and 120, it is fed through lines 166 and 176into line 180. Line 180 then meets tubular receiver 220. Inside tubularreceiver 220, the liquid is maintained at the elevated pressure where aportion of the microorganisms are killed by being maintained under ahigh pressure for a sufficient period of time (e.g. about 100 to about500 seconds). To keep this treatment process continuous, the flow of theliquid is continuous through the tubular receiver. The length of thetubular receiver will depend on, among other things, flow rates,dimensions, and the amount of the time needed for the desired killlevel. The times provided herein may be lengthened, or shortened,depending on, among other things, initial microbial levels and desiredkill levels.

As shown in FIG. 5, receiver 220 can be of autoclave or tubular design,and will be of a compound construction with an outer pressure tubing 222and a thin wall liner of corrosion resistant stainless steel 224. Outerpressure tubing 222 comprises ASTM standard 4340 steel with an innerbore face 222a having a diameter about 2.5 inches and outer face 222bhaving a diameter measuring about 6.5 inches, however any composition ofpressure tubing meeting the strength requirements may be used.

Inner liner 224 may consist of Type 304 stainless steel tubing havinginner bore surface 224a having a diameter measuring approximately 2.0inches, and outer surface 224b having a diameter measuring 2.375 inches.Inner liner 224 will be slipped inside of inner bore 222a of outerpressure tubing 222 and will be hydraulically expanded via anautofrettage process to tight fit to the 2.5 inch inside diameter ofbore 222a. The purpose of the stainless steel liner is to providecorrosion resistance against the PH of the liquid being treated and tobe compatible with the requirements of food processing.

The system may also be provided with safety mechanisms to prevent therupture or tear of any of the lines or components within the system,therefore an additional embodiment of the invention is shown in FIG. 6.FIG. 6 discloses a rupture disk 212 attached to line 72 before line 72connects to surge drum 76. Rupture disk 212 is set to rupture at about40,000 psig and thereby warning any operator of the system that thepressure of the liquid component in line 72 or surge tank 76 hasexceeded about 40,000 psig. In addition, another rupture disk 214 isconnected to line 180 as line 166 joins line 180. Rupture disk 214 isset to rupture at about 65,000 psig and thereby warning any operator ofthe system that the pressure of the liquid component in line 180 hasexceeded about 65,000 psig. Line 180 then connects to tubular receiver220. On the other side of tubular receiver 220, is line 228 connectedthereto. Connected to line 228 is automatic shutdown controller 229which shuts the system down if the pressure in the system breaks eitherrupture disk.

As shown in FIG. 3 Line 228 connects to heat exchanger 250. This heatexchanger reduces the temperature of the pressurized liquid from about83 degrees Fahrenheit to about 35 degrees Fahrenheit. In addition,connected to line 228 is pressure let down station 240 as shown in FIG.7. Pressure let-down station 240 actually consists of an alternatingseries of pressure let-down controllers 242a, 242b, 242c each in analternating series with heat exchangers 244a, 244b, and 244c followed bypressure control valve 248 which combine to reduce the pressure in theliquid to atmospheric pressure by a series of steps while keeping thetemperature of the liquid component at or below about 85 degreesFahrenheit. Line 228 links the pressure let down controllers to the heatexchangers in this series.

Pressure let down controllers 242a, 242b, and 242c each comprise apressure control valve 260 (FIG. 8) or a flow control orifice 280 (FIG.9). FIG. 8 shows that pressure control valve 260 is comprised of a valvebody 262, with valve stem 264 housed within the valve body 262. Valvestem 264 is secured within valve body 262 by gland 266 and valve stem264 is supported inside valve body 262 by packing 268.

Valve seat 269 rests against valve stem 264 inside valve body 262. Thelines in the system are made up of pressure tubing 222 and liner 224which rests against valve seat 269 inside valve body 262. Pressuretubing 222 and liner 224 are secured within valve body 262 by clampingblock 274 and bolts 276 and 278 which secure clamping block 274 to valvebody 262.

FIG. 9 shows the cross sectional view of flow control orifice 280 whichis spliced between two sections of pressure tubing 222 and liner 224which ultimately form line 228. Flow control orifice comprises two hubs282 and 284 which are threaded around pressure tubing 222. Clamps 286and 288 clamp hubs 282 and 284 together and force both ends of pressuretubing line 228 into collar 290. Collar 290 supports sapphire orifice291 and gland 292 which is threaded into collar 290 after sapphireorifice 291. The minimum diameter of this flow control orifice 280 isabout 0.2 inches which is large enough to pass any particulate what maybe flushed out during a clean-in-place washing of the process equipment.

The design of the orifice controller and the downstream tubing is suchthat at the discharge of the orifices, eddies are created downstream ofthe orifice with the eddies assisting in the absorption of the kineticenergy of the jet stream.

Maintenance or replacement of an orifice may be required from time totime. Therefore, the installation of double block valves may be providedwithin the system just prior to the pressure let down station toperiodically replace certain sections of the system without reducing thepressure in the system. It is important to maintain a constant pressurein this system to avoid a cycling of the system which may result in ashorter life of the components.

While the liquid component is compressed in tubular receiver 220, thepressure in the system reduces the liquid component to about 87.5% ofits original volume. When the liquid component reaches the pressure letdown stage, it is expanded to its original volume through a series ofsteps. In this case, the expansion of the liquid occurs through areverse Joule-Thompson effect, whereby the liquid will heat up duringeach pressure let down step. To maintain the quality of the liquid (e.g.orange juice) in the apparatus, the heat exchanger following eachpressure relief valve will keep the temperature of the liquid belowabout 85 degrees Fahrenheit. Thermodynamically, the expansion acrosseach pressure let-down controller is shown in FIG. 10.

For example, the cooled liquid component enters pressure let downcontroller 242a with a temperature of about 35 degrees Fahrenheit and apressure of about 60,000 psig. Pressure let down controllersimultaneously decreases the pressure of the liquid to about 41,000while increasing the temperature to about 85 degrees Fahrenheit. Theliquid then enters heat exchanger 244a where it is cooled back to atemperature of about 35 degrees Fahrenheit. The liquid then enterspressure let down controllers 242b. Pressure let down valvesimultaneously decreases the pressure of the liquid to about 21,000while increasing the temperature of the liquid to about 85 degreesFahrenheit. Heat exchanger 244b then cools the liquid back to about 35degrees Fahrenheit. Next, the liquid enters pressure let down controller242c where the pressure is further reduced to about 1,500 psig while theliquid again heats up to about 85 degrees Fahrenheit. Heat exchanger244c cools the liquid back to about 35 degrees Fahrenheit. While thefirst three pressure reductions work under the reverse Joule ThompsonEffect the last pressure reduction does not. Accordingly, when theliquid enters pressure control valve 248 the pressure is reduced toabout 14.5 psig without any noticeable temperature increase. The flowrates across pressure let down controllers 242a, 242b, and 242c areabout 2,000 ft/sec, about 1,500 ft/sec, and about 1,000 ft/secrespectively. These flow rates across the pressure let down controllersare sufficient to cause the remaining microorganisms within the liquidcomponent to fracture and thereby facilitate the sterilization of theliquid component.

The liquid component then moves down line 228 and into mixing tee 293(FIG. 7). Mixing tee 293 connects to line 294 which then splits intolines 295 and 296 having valves 295a and 296a respectively. In addition,mixing tee 293 connects to pulp slurry line 297. Pulp slurry line 297has valve 297a and connects to pulp slurry pump 298. Pulp slurry pump298 is fed by pulp slurry line 299. Therefore, the liquid componentmixes with the particulate component in mixing tee 297 and then flows topackaging down line 294 and then down line 296.

In following with the standards of the industry, the high pressureliquid treatment system may be periodically flushed, with a solvent(e.g. hot water) to remove the build-up of any particulate or coatingsof components by the liquid food. The solvent can be an acid wash but itshould be chemically compatible with the equipment. To avoid unnecessarycycling in the system, the operating pressures within the system aremaintained while the fluid feed in the system is changed over from theliquid component of liquid food to a solvent. Therefore, to flush thesystem of particulates, valve 10a on line 10 (FIG. 2) is closed whilevalve 14a on line 14 is opened. This step stops the flow of the liquidcomponent into the system, and allows a solvent or in this case, hotwater to feed into the system. Hot water feeds into the system at 180degrees Fahrenheit and 20 psig into line 14 from hot water tank 16.Using standard or above standard operating pressures, the hot water ispumped through the system to free particulates from the system. Thewater flows through the system by the same process as described abovefor the liquid component of the untreated liquid food. Liquid componenttreatment system 1 has a volume of approximately 400 gallons. Tocompletely flush the system of particulates, it is necessary to flush upto eight volumes of hot water through the system before normalactivities can resume. To avoid having hot water contaminate thepackaging system, valves 295a and 297 on line 295 and 297 respectivelyare closed while valve 296a on line 296 is opened to allow the hot watertreatment to flow through the system and down line 296 instead of line295. The system may be flushed with hot water once every 24 hours andthen returned back to treating the liquid component of the liquid food.

Sterilizing the Particulate Component

FIG. 11 discloses the batch process for sterilizing the particulatecomponent of the liquid food as shown in step D of FIG. 1. Although thisbatch process is described in connection with the particulate component,the liquid component can also be treated with this batch process, aloneor in combination with the previously described continuous process.

Step D1 involves introducing the particulate component into apressurized system. In Step D2, the pressure on particulate component inthe system is increased to about 40,000 psig to about 60,000 psigwhereby the temperature of the particulate component in the system willincrease by approximately 20 degrees Fahrenheit. Next, step D3 involvesholding the particulate component at a constant pressure for aproscribed period of time (e.g. about 100 to about 300 seconds) whichwill sterilize the particulate component by killing off microorganismsin the particulate component. Step D4 involves rapidly reducing thepressure on the particulate component to atmospheric pressure. Duringthis rapid pressure reduction step, a portion of the liquid particulatecomponent may reach temperatures as high as about 240 degrees Fahrenheitand maintain an average temperature of about 125 degrees Fahrenheit thusexceeding the desired temperature range for the product. Another portionof the particulate component will remain within the desired temperaturerange of about 35 to about 85 degrees Fahrenheit. Therefore, step D5involves separating the high temperature particulate component from thelow temperature component. In step D6 the high temperature liquidparticulate component is transferred to an off site tank. Next, step D7involves transferring the treated low temperature particulate componentproduct to a liquid component and particulate component mixer.

To fully treat the particulate component in the process described above,the particulate component is sent to a particulate treatment system 300.This system may be comprised of a single receiver treatment system 310in FIG. 12 or a double receiver treatment system 400 in FIG. 13. Ineither of these systems, the particulate component of the liquid is heldat an elevated pressure of about 60,000 psig for a prescribed length oftime (e.g. about 100 to about 300 seconds) to deactivate microorganismsthat may be present in the particulate component.

FIG. 12 shows the single receiver system 310. This high pressureparticulate system comprises a series of lines 312, 314, 316, 318, 320,322 and 324 which connect feed tank 330, intensifier 340, bleed tank350, product tank 360, and receiver 370 together and allow theparticulate component to flow between them.

Line 312 which comprises valve 312a and temperature gauge 312b connectsfeed tank 330 to receiver 370. Line 314 which comprises valve 314aconnects product tank 360 to line 312 between valve 312a and receiver370. Vent line 316 extends from receiver 370 and contains pressure gauge316a, valve 316b, and pressure control valve 316c. Nitrogen line 318contains pressure control valve 318a, and valve 318b and connects tovent line between valve 316b and receiver 370. Line 320 which comprisestemperature gauge 320a, pressure gauge 320b and valve 320c, connectsintensifier 340 to line 316 between valve 316b and receiver 370. Line322 includes valve 322a, temperature gauge 322b and valve 322c connectsbleed tank 350 to vent line 316 between valve 316b and receiver 370.Line 324 connects to intensifier 340 to allow pressurizing liquid toflow into intensifier 340.

Included in this sterilizing system 310 is a system of blanketing gaswhich is used in all tanks to protect the particulate component fromoxidation. Blanketing gas pressure can also be used as a motive force toassist the gravity flow of the particulate component from one tank toanother. In the single receiver configuration 310 (FIG. 12), each vesselhas a separate source of chemical grade nitrogen and a pressure ventvalve. In the multi-receiver configuration 400 (FIG. 13), each tank andreceiver has a dedicated nitrogen system for blanketing gas and gasassisted feed and product transfers.

For example, connected to feed tank 330 is feed line 332 having valve332a and vent line 334 having pressure control valve 334a. Vent line 334connects to nitrogen line 336 having pressure control valve 336a.Pressure control line 337 connects pressure control valve 334a on ventline 334 to pressure control valve 336a on nitrogen line 336. Also,connected to feed tank 330 is pressure gauge 338 and temperature gauge339 for reading the pressure and temperature of the particulate matterin the feed tank.

Connected to bleed tank 350 is product line 352 having valve 352a andvent line 354 having pressure control valve 354a. Vent line 354 connectsto nitrogen line 356 having pressure control valve 356a. Pressurecontrol line 357 connects pressure valve 354a on vent line 354 topressure control valve 356a on nitrogen line 356. Also connected tobleed tank 350 is pressure gauge 358 and temperature gauge 359 forreading the pressure and temperature in the bleed tank.

Connected to product tank 360 is product line 299 (FIG. 2) having valve299a, and vent line 364, having pressure control valve 364a. Vent line364 connects to nitrogen line 366 having pressure control valve 366a.Pressure control line 367 connects pressure control valve 364a on ventline 364 to pressure control valve 366a on nitrogen line 366. Alsoconnected to product tank 360 is pressure gauge 368 and temperaturegauge 369 for reading the pressure and temperature in the bleed tank.

Receiver 370 as shown in FIGS. 12 and 14 includes temperature controlgauge 372, connected to thermocouple 374 which is housed within tubing376. In addition, conductivity cell 378 is located within receiver 370to detect whether receiver 370 has filled with particulate component. Asshown in FIG. 14 a cross-sectional representation of receiver 370 showsthe receiver itself comprises an outer casing 380, and an inner casing382. Inner casing 382 has an inner wall 382a and an outer wall 382b.Inner casing 382 is substantially cylindrical in shape, but it angles inat a 45 degree angle at both a bottom end 384, and a top end 386. Bothbottom end 384 and top end 386 taper to ducts 388 and 390 respectively.Bottom end 384 is supported within outer casing 380 by bottom plug 392.Top end 386 is supported within outer casing 380 by top plug 394.

To process the particulate component using the system 310, bulkuntreated particulate component slurry is fed into elevated feed tank330. The slurry has a concentration in the range of 40% to 60% andpreferably about 50% particulate matter with the balance being anuntreated liquid component. This concentration of approximately 50% pulpand 50% liquid facilitates reasonably rapid transfers of the slurry fromtank to tank. Other less or more concentrated slurries of particulatematter can be used, with more concentrated particulate slurriesrequiring positive displacement. This mixture is fed through feed line332 into feed tank 330. As feed tank 330 fills, nitrogen blanketing gasleaves feed tank 330, and vents through line 334. As the untreatedmixture leaves feed tank 330, nitrogen blanketing gas is then fed backinto feed tank 330 via nitrogen line 336.

The untreated mixture is fed by gravity flow out of feed tank 330through line 312 and into a lower end of receiver 370, filling receiver370 from the bottom up. To prevent any degradation of the particulatecomponent, receiver 370 is filled with a blanketing gas (preferablynitrogen) that is displaced out of receiver 370 as the tank is filledwith particulate matter. The displaced nitrogen gas from receiver 370flows through line 316 to vent. When the receiver is completely full, asindicated by conductivity cell 378, or other suitable means, flow fromthe particulate component is stopped by closing valve 312a in line 312.Valves 316b in line 316, and 322a in line 322 are then closed. Anuntreated liquid component is introduced into the system via line 324.The untreated liquid is next pumped through intensifier 340 and placedinto line 320. The liquid feeds into receiver 370 and the receiver ispressurized by intensifier 340 forcing the liquid component through thesystem. The system is then pressurized by intensifier 340 between about40,000 and about 60,000 psig. When the intensifier discharge pressureand the receiver pressure reaches its target pressure the pressurizationis discontinued, and valve 320c in line 320 is closed. Duringpressurization, the temperature of the particulate component in thereceiver will increase slightly (e.g. by about 20 degrees Fahrenheit).The liquid in the filled and pressurized receiver is then allowed tostand, under pressure, for a prescribed residence time (e.g. about 100to about 300 seconds) which will cause the deactivation of themicroorganisms in the pressurized slurry of particulate and liquidcomponent. After expiration of the prescribed residence time (e.g. up toabout 300 seconds), valves 322a and 322c in line 322 are opened,allowing the pressure in receiver 370 to be vented to bleed tank 350.This vented liquid slurry, being the last used to pressurize thereceiver, causes the pressure in the receiver to be rapidly reduced toessentially atmospheric pressure. The pressure drop is via isenthalpicexpansion, causing the initial temperature of the vented fluid to reachtemperatures as high as about 240 degrees Fahrenheit. The temperature ofthe vented liquid will gradually decrease as the pressure in the ventedreceiver decreases, dropping to about 50 degrees Fahrenheit at the endof the depressurization. However, the average temperature of the ventedliquid stream is about 125 degrees Fahrenheit, exceeding its maximumallowed temperature. The liquid accumulated in bleed tank 350 havingexceeded the maximum allowable temperature, is therefore designed aslower valued premium product and is transferred to an off-site tank forlater use in a lesser valued product.

The treated particulate component slurry is discharged from receiver 370to product tank 360 by opening valve 314a on line 314 and allowing freshblanketing gas from nitrogen line 318 to displace the lost volume inreceiver 370. The rate of transfer may be accelerated by increasing thepressure of the blanketing nitrogen gas. As the slurry flows intoproduct tank 360, the displaced blanketing gas in product tank 360 ventsto the atmosphere via vent line 364. Next, the particulate componentflows down line 299 to mix with the liquid component (FIG. 3). No mixeris needed if the liquid component is treated with the batch processalone.

As an example of this process, using a 16"×81" receiver, five 700 lbbatches of particulate component (e.g. pulp) each containing about 350lb of both liquid food and particulate component can be deactivated perhour. The cycle time of about 12 minutes per batch includes the time forcharging the receiver, pressurizing it, holding it for a prescribedresidence time, venting the pressure and transferring the treatedproduct to product tank 360. The transfer times may be altered bychanging the viscosity of the particulate component or by using anitrogen gas assist. Altering the viscosity can be done by an increaseor a reduction of the liquid content of the particulate component.

Each 700 lb batch of particulate component slurry will process about 350pounds of particulate component (e.g. pulp), which will produce about3500 lb/hr, or about 401 gallon/hr of final brix 12 blended product. Theabove dimensioned single reactor configuration will produce about 1,750lb. of particulate component/hour compared to a need for about 6,282lbs/hr to process about 100 gpm of liquid component (e.g. juice). Thus,to meet the higher capacity liquid component treatment system, eitherthe size of the receiver must be increased or additional receivers mustbe installed.

Multi-Receiver Configuration

The multi-receiver system 400 (FIG. 13) differs from the single receiversystem in that the multi-receiver system contains an additional receiver402 and a different set of lines connecting feed tank 330, intensifier340, bleed tank 350, product tank 360 to first receiver 370, and secondreceiver 402. In the multi-receiver system, line 410 contains pressurevalve 410a and connects feed tank 330 to intensifier 340. In addition,connected to line 410 are lines 412 and 414 which connect line 410 toreceiver lines 416 and 418 respectively. Line 412 contains valve 412awhile line 414 contains valve 414a. Receiver line 416 extends fromreceiver 370 to product line 420 and comprises valves 416a and 416bconnected to receiver line 416 on either side of line 412. In addition,receiver line 418 extends from receiver 402 to product line 422 andcontains valves 418a and 418b located on line 418 on either side of line414. Product line 420 feeds into product line 422 wherein product line422 then feeds into product tank 360.

Line 430 extends from intensifier 340 and contains temperature gauge430a. Line 430 splits into two lines 434 and 438. Line 434 containsvalve 434a and pressure gauge 434b and connects line 430 to receiverline 440. Line 438 contains valve 438a and pressure gauge 434b andconnects line 430 to receiver line 442. Receiver line 440 and receiverline 442 connect to receiver 370 and receiver 380 respectively. Receiverline 440 contains first pressure valve 440a, second pressure valve 440b,and pressure control valve 440c. Receiver line 442 contains firstpressure valve 442a, second pressure valve 442b and pressure controlvalve 442c. Line 450 connects receiver lines 440 and 442 and contains afirst valve 450a, a first pressure control valve 450b, a second pressurecontrol valve 450c and a second valve 450d. In addition, connected toline 450 between pressure control valve 450b and 450c is nitrogen inputline 452.

Line 460 connects receiver lines 440 and 442 to bleed tank 350. Line 460contains valve 460a, temperature gauge 460b, and valve 460c. Valve 460ais located between receiver lines 440 and 442, while temperature gauge460b and valve 460c are located on line 460 between receiver line 442and bleed tank 350. The dual receiver operation starts when theuntreated particulate component leaves elevated feed tank 330 andtravels down line 410 by gravity, through line 412, entering line 416where it flows into first receiver 370. Valve 410a is closed preventingparticulate component from entering intensifier 340. As the particulatecomponent enters the bottom of receiver 370, nitrogen blanketing gasleaves receiver 370 and vents through line 440. When receiver 370 fillsto the top, valves 412a, 416a, and 440a close. Once receiver 370 is fullits pressure is increased with raw particulate component (e.g. pulp)from feed tank 330. Valve 410a opens and the raw particulate componentflows from feed tank 330 though line 410 and into intensifier 340.Intensifier 340 pumps the particulate component into line 430, throughline 434, and into receiver 370. During pressurization to thedeactivation pressure, the temperature of the particulate component inreceiver 370 will reach about 51 degrees Fahrenheit which is well withinthe preferred product temperature range of about 35 degrees Fahrenheitto about 85 degrees Fahrenheit. After receiver 370 reaches its targettreatment pressure, the flow from intensifier 340 is stopped and valve434a is closed to lock the particulate component in receiver 370 for atreatment time of 100 to 300 seconds at a pressure between about 40,000to about 60,000 psig.

As the first receiver tank 370 sterilizes a batch, valve 410a closes butvalve 414a opens to allow an additional batch to flow by gravity fromfeed tank 330 into line 414, next into line 418, flowing into the bottomof second receiver 402. As second receiver 402 fills with theparticulate component, nitrogen blanketing gas leaves receiver 402 andvents through line 442. When receiver 402 fills to the top, valves 414a,418a and 442a close. Once receiver 402 is full, its pressure isincreased with raw particulate component (e.g. pulp) from feed tank 330.Valve 410a now opens allowing the raw particulate component from feedtank 330 to flow through line 410 and into intensifier 340. Intensifier340 pumps the particulate component through line 430, into line 438 andthen into the top of receiver 402. During pressurization to thedeactivation pressure, the temperature of the particulate component inreceiver 402 will reach approximately 51 degrees Fahrenheit which iswell within the product temperature range of about 35 degrees Fahrenheitto about 85 degrees Fahrenheit. After receiver 402 reaches its targettreatment pressure, the flow from intensifier 340 is stopped and valve438a is closed to lock the particulate component in receiver 402 for atreatment time of about 100 to about 300 seconds at a pressure betweenabout 40,000 and about 60,000 psig.

Once second receiver 402 is pressurized to the deactivation pressure,the procedure for discharging treated particulate component fromreceiver 370 is started. The pressure in receiver 370 is reduced fromabout 60,000 psig to atmospheric by venting the receiver pressure vialines 460 and 462 to bleed tank 350. This is achieved by opening valves440a, and 460a, on lines 440, and 460 respectively. In the pressure letdown stage, the temperature of the vented stream will reach 240 degreesFahrenheit making it unsuitable for use as a premium blend stock. Thetemperature of the treated particulate component in receiver 370 asmeasured by the bottom mounted thermocouple settles at about 38 degreesFahrenheit after depressurization. The treated particulate component inreceiver 370 is also at about 38 degrees Fahrenheit. Next, valves 416aand 416b on line 416 now open and allow the treated particulatecomponent to flow through lines 416, 420 and 422 to product tank 360 bygravity, or a possible blanketing gas (e.g. nitrogen) assist. Duringthis transfer, receiver 370 is refilled with blanket gas (e.g.nitrogen). After emptying receiver 370, the system is ready forrefilling again with raw untreated particulate component.

During the pressure treatment of the second batch particulate componentin receiver 370, the cycle starts over again with the draining andrefilling of receiver 402. As in the draining of receiver 370, thepressure in receiver 402 is reduced from about 60,000 psig toatmospheric by venting the receiver pressure via lines 442, and 460 tobleed tank 350. This is achieved by opening valve 442a in line 442. Thetemperature of the vented stream can reach about 240 degrees Fahrenheitmaking it unsuitable for premium blend stock. However, the temperatureof the treated particulate component in receiver 402 remains at about 38degrees Fahrenheit after depressurization. Next, valves 418a and 418b online 418 open and allow this treated particulate component to flowthrough lines 418 and 422 to product tank 360 by gravity with a possibleblanketing gas (e.g. nitrogen gas) assist.

Like the single receiver configuration, the multi-receiver configurationalso utilizes a system blanketing gas (e.g. nitrogen) so that at no timeare the vessels and piping exposed to atmospheric contamination oroxidizing atmospheres.

The dimensions and capacity of the receiver configurations can be variedwith a change in internal diameter or length of the receiver and thetensile strength of the steel, as equipment or process costs dictate.

In another embodiment of the invention, the particulate component may betreated in a multi-receiver system using more than two receivers forprocessing. If two or more receiver vessels are used, then each receivervessel is filled alternately such that as one receiver vessel ispressurized, the other receiver vessel is being depressurized andrefilled with the next batch.

The lines in the system are comprised of short segments of pressuretubing 222 to allow periodic replacement of the lines in the system,short segments of pressure tubing 222 are coupled together using agreylock coupling 500 as shown in FIG. 15. FIG. 15 shows a crosssectional view of greylock coupling 500 which comprises two hubs 510 and520 coupled together by clamps 530 and 540 having bolts 532 and 534 onclamp 530 and bolts 542 and 544 on clamp 540. Hubs 510 and 520 threadonto each end of spliced pressure tubing 222. Seal ring 550 fits betweenthe two spliced ends of pressure tubing 222 and inner liner 224. The twoends of pressure tubing 222 and liner 224 are joined together to formlines in the system by placing clamps 530 and 540 around hubs 510 and520. Bolts 532 and 534 are tightened on clamp 530 to secure clamp 530 tohubs 510 and 520. Bolts 542 and 544 are tightened on clamp 540 to secureclamp 540 to hubs 510 and 520. The tightening of these bolts brings thetwo pieces of pressure tubing together to form a tight seal around sealring 550. If it is necessary to remove a piece of pressure tubing from aline, then bolts 532 and 534 are loosened on clamp 530 and bolts 542 and544 are loosened on clamp 540, allowing pressure tubing 222, whichhouses liner 224, to be removed from the line.

To close off a line, FIGS. 16 and 17 disclose a cross sectional view ofpressurization end plugs having two different designs. In both designsthere is a coupling 610 threaded around pressure tubing 222. Coupling610 comprises a flange bolt hole 614 and a flange 618. An end portion ofpressure tubing 222 is cut away to allow ring 620, housed withincoupling 610 to contact inner liner 224.

In the first design, plug 640 (FIG. 16) has a stopper portion 642 and athreaded portion 648. Threaded portion 648 threads within coupling 610and stopper portion 642 fits within inner liner 224. Notch 650 is cutwithin stopper portion 642 with notch 650 for housing ring 652. Plug 640has a inner channel 660 which leads to pressure ring 662. Above pressurering 662 is an open channel 664.

In the second design, plug 670 (FIG. 17) has a stopper portion 672 and athreaded portion 678. Threaded portion 678 threads within coupling 610and stopper portion 672 fits within inner liner 224. Notch 680 is cutwithin stopper portion 672 with notch 680 for housing ring 682.

The liquid of this process may be, among other things; orange juice. Thepressure vessels and the intensifier discharge lines should befabricated from high pressure metal alloys such as 4340, 13-8PH, 15-5PH,and 17-48 PH precipitation hardened steels. The high pressure vesselsand lines are lined with stainless steel to protect the quality of theproduct and to preclude corrosion by the pH of the liquid or particulatecomponent. The low pressure tanks, transfer lines and valves arefabricated of stainless steel to protect the quality of the product andto preclude corrosion of the hardware.

Although the present invention has been described in detail, it shouldbe understood that various modifications, alterations, and substitutionscan be made to this description without departing from intended scope ofthe present invention as defined by the appended claims.

What is claimed is:
 1. A process for sterilization of a liquid in acontinuous system comprising:a) substantially continuously pumping theliquid through a pressurized system; b) increasing the pressure of theliquid at a plurality of pressurization stages; c) maintaining theliquid at an elevated pressure for a predetermined period of time; d)incrementally decompressing the liquid in a plurality of increments tofracture microorganisms within the liquid, the incrementscomprising:reducing the pressure in the liquid from about 60,000 psig toabout 41,000 psig; reducing the pressure in the liquid from about 41,000psig to about 21,000 psig; reducing the pressure in the liquid fromabout 21,000 psig to about 1,500 psig, reducing the pressure in theliquid from about 1,500 psig to about 15 psig; and e) maintaining thetemperature of the liquid within a desired temperature range during theincrementally decompressing of the liquid.
 2. The process of claim 1,wherein increasing the pressure comprises introducing the liquid into anintensifier.
 3. The process of claim 1, wherein the liquid is maintainedat the elevated pressure for at least 100 seconds.
 4. The process ofclaim 1, wherein pressure is increased at two stages.
 5. The process ofclaim 1 wherein incrementally depressurizing the liquid and maintainingthe temperature of the liquid further comprises an alternating series ofsteps of:cooling the liquid to a desired temperature; depressurizing theliquid to a desired reduced pressure level; and repeating the coolingand depressurizing, steps to reach a desired level of reduced pressurein the liquid while maintaining the liquid in a desired temperaturerange.
 6. An apparatus for the continuous sterilization of a liquid in apressurized system comprising:a pump for continuously introducing theliquid into the pressurized system; a first stage intensifier coupled tothe pump the first stage intensifier for increasing the pressure of theliquid in the system; a second stage intensifier coupled to the firststage intensifier, the second stage intensifier for receiving andincreasing the pressure of the pressurized liquid in the system; apressure receiver coupled to the second intensifier, the pressurereceiver for receiving the pressurized liquid from the second stageintensifier and maintaining the pressurized liquid for a predeterminedperiod of time; a pressure reducer coupled to the pressure receiver,said pressure reducer comprising a liquid temperature controller and apressure controller wherein the pressure reducer reduces the pressure ofthe liquid in the pressurized system to a predetermined level whilemaintaining the liquid within a desired temperature range; and a surgetank coupled to the first stage intensifier for recycling a portion ofthe liquid component back to the first stage intensifier.
 7. Theapparatus of claim 6, wherein the pressure reducer comprises analternating series of heat exchangers and pressure controllers.
 8. Theapparatus of claim 6, wherein said liquid temperature controllercomprises a series of heat exchangers that maintain the temperature ofthe liquid between about 35 degrees Fahrenheit and about 85 degreesFahrenheit.
 9. The apparatus as in claim 6, further comprising a liquidcomponent and particulate component separator connected to the liquidpump for separating particles from the liquid.
 10. An apparatus for thecontinuous sterilization of a liquid in a pressurized systemcomprising:a pump for continuously introducing the liquid into thepressurized system; a first stage intensifier coupled to the pump, thefirst stage intensifier for increasing the pressure of the liquid in thesystem; a second stage intensifier coupled to the first stageintensifier, the second stage intensifier for receiving and increasingthe pressure of the pressurized liquid in the system, a pressurereceiver coupled to the second intensifier, the pressure receiver forreceiving the pressurized liquid from the second stage intensifier andmaintaining the pressurized liquid for a predetermined period of time; apressure reducer coupled to the pressure receiver, said pressure reducercomprising a liquid temperature controller and a pressure controller,wherein the pressure reducer reduces the pressure of the liquid in thepressurized system to a predetermined level while maintaining saidliquid within an acceptable temperature range, comprising a particulatetreatment apparatus coupled to the separator, the treatment apparatuscomprising: and a liquid component and particulate component separatorconnected to the liquid pump for separating particles from the liquid; apressure treatment receiver vessel for sterilizing particulate slurry;an intensifier coupled to the receiver vessel for increasing thepressure on the particulate slurry; a recoverer for collecting thetreated particulate slurry; and a blender for blending the treatedparticulate slurry with the treated liquid matter.
 11. The apparatus asin claim 10, wherein there are at least two pressure treatment receivervessels for sterilizing the particulate slurry, the vessels connected tothe liquid component and particulate slurry separator.
 12. A process forsterilization of a liquid in a continuous system comprising:a)substantially continuously pumping the liquid through a pressurizedsystem; b) increasing the pressure of the liquid at a plurality ofpressurization stages; c) maintaining the liquid at an elevated pressurefor a predetermined period of time; d) depressurizing the liquid tofracture microorganisms within the liquid; e) separating the liquid froma particulate slurry; f) treating the particulate, slurry in apressurized system by:i) increasing the pressure on the particulateslurry; and ii) returning the particulate slurry to substantiallyatmospheric pressure; and g) blending the particulate slurry with theliquid slurry.
 13. The process of claim 12 wherein in step i) theparticulate slurry is treated in a plurality of receiver vessels.
 14. Anapparatus for the continuous sterilization of a liquid in a pressurizedsystem comprising:a pump for continuously introducing the liquid intothe pressurized system; a first stage intensifier coupled to the pump,the first stage intensifier for increasing the pressure of the liquid inthe system; a second stage intensifier coupled to the first stageintensifier, the second stage intensifier for receiving and increasingthe pressure of the pressurized liquid in the system; a pressurereceiver coupled to the second intensifier, the pressure receiver forreceiving the pressurized liquid from the second stage intensifier andmaintaining the pressurized liquid for a predetermined period of time; apressure reducer coupled to the pressure receiver wherein the pressurereducer reduces the pressure of the liquid in the pressurized system toa predetermined level; a liquid component and particulate componentseparator connected to the liquid pump for separating particles from theliquid; a particulate treatment apparatus coupled to the separator, thetreatment apparatus comprising:a pressure treatment receiver vessel forsterilizing particulate slurry; an intensifier coupled to the receivervessel for increasing the pressure on the particulate slurry; arecoverer for collecting the treated particulate slurry; and a blenderfor blending the treated particulate slurry with the treated liquidmatter.
 15. The apparatus as in claim 14, wherein there are at least twopressure treatment receiver vessels for sterilizing the particulateslurry, the vessels connected to the liquid component and particulateslurry separator.
 16. A process for sterilization of a liquid in acontinuous system comprising:a) substantially continuously pumping theliquid through a pressurized system; b) increasing the pressure of theliquid at a plurality of pressurization stages; c) maintaining theliquid at an elevated pressure for a predetermined period of time; d)incrementally decompressing the liquid in a plurality of increments tofracture microorganisms within the liquid; e) maintaining thetemperature of the liquid within a desired temperature range during theincrementally decompressing the liquid; f) separating the liquid from aparticulate component; and g) treating the particulate component in apressurized system by:i) increasing the pressure on the particulatecomponent; and ii) returning the particulate matter to substantiallyatmospheric pressure; and h) blending the particulate component with theliquid component.
 17. The process of claim 16 wherein in step i) theparticulate component is treated in a plurality of receiver vessels. 18.The process of claim 16, wherein the step of returning the particulatematter to substantially atmospheric pressure comprises incrementallydecompressing the particulate matter in a plurality of increments tofracture microorganisms within the particulate component and maintainingthe temperature of the particulate component within a desiredtemperature range during the incrementally decompressing of theparticulate component.